US2970893A - Production of lime and hydropgen sulfids - Google Patents

Production of lime and hydropgen sulfids Download PDF

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US2970893A
US2970893A US743050A US74305058A US2970893A US 2970893 A US2970893 A US 2970893A US 743050 A US743050 A US 743050A US 74305058 A US74305058 A US 74305058A US 2970893 A US2970893 A US 2970893A
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catalyst
lime
gas
hydrogen sulfide
steam
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Prentiss S Viles
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ExxonMobil Technology and Engineering Co
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/16—Hydrogen sulfides
    • C01B17/164—Preparation by reduction of oxidic sulfur compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/02—Oxides or hydroxides
    • C01F11/08—Oxides or hydroxides by reduction of sulfates

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  • the present invention is directed to a method for producing lime and hydrogen sulfide. More particularly, the invention is concerned with the production of lime and hydrogen sulfide from gypsum. In its more specific aspects, the invention is directed to a catalytic method for producing lime andhydrogen sulfide at a substantially reduced temperature.
  • the present invention may be briefly described as a i method for producing lime and hydrogen sulfide which comprises forming a mixture of calcium sulfate and a sulfur-resistant catalyst and then contacting the mixture with a hydrocarbon gas and steam at a temperature within the range from about 850 to about 1500l F. in the absence of free oxygen, the gas and steam being present in amounts in excess of theoretical to form lime and hydrogen sulfide.
  • the hydrogen sulfide and lime are separated from the catalyst and recovered and the recovered lime is then cooled in the absence of free oxygen.
  • the catalyst employed in the practice of the present invention is a sulfur-resistant catalyst which may be exemplified by cobalt molybdate.
  • Other suitable sulfurresistant catalysts may be used, such as reducible salts of molybdenum and cobalt.
  • the sulfur-resistant catalyst is employed on a suitable support or carrier.
  • a suitable support or carrier for example, cobalt molybdate in an amount of 12 to 15 percent by weight deposited on a suitable carrier or support, such as alumina, is eminently suitable as a catalyst.
  • the catalyst may comprise an amount within the range from about 1 to about 99 percent by weight of the active catalytic material with the remainder being the support.
  • alumina which may be a substantially purified alumina, such as gamma alumina
  • suitable supports may be zirconia, magnesia, and other materials, such as clay,;
  • the temperatures employed in the practice of the present invention may range from about 850 to about 1500 F., with a preferred temperature in the range from about 1200 to l400 F.
  • a sulfur-re sistant catalyst By virtue of employing a sulfur-re sistant catalyst, it is possible to produce lime and hydrogen sulfide at substantially reduced temperatures over that possible heretofore using a hydrocarbon gas.
  • Pressures suitably may range from about to about 1000 ⁇ pounds per square inch gauge.
  • pressures may range from about l0 up to about 200 pounds per square inch gauge.
  • the hydrocarbon gas employed in the practice of the present invention is suitably natural gas or the gaseous components thereof, such as methane, ethane, propane, and butane. It is preferred to use natural gas, although methane and the other gaseous components may be used.
  • numeral 11 designates a charge line by way of which a gaseous hydrocarbon, such as methane, is introduced into the system by opening l valve 12. Discharging into line 11 is a charge line 13,
  • valve 14 by way of which steam is introduced in admixture with the methane.
  • the steam and methane mixture then fiows into a furnace 15 provided with a heating coil 16 and gas burners 17, which raise the temperature of the mixture to a temperature in the range from about 850 to about 1500 F.
  • the heated mixture fiows by way of line 18 into a large conduit 19 into which is introduced by way of line 20 a sufiicient amount of catalyst, such as cobalt molybdate on alumina, the catalyst being carried through line 19 by the velocity of flow of the mixture of methane and steam.
  • catalyst such as cobalt molybdate on alumina
  • the catalyst is admixed in line 19 with powdered gypsum introduced thereto by way of line 21, and the mixture of catalyst and powdered gypsum are then flowed by way of line 19 into a reaction zone 22, which is a large vessel provided with a cone-shaped member 23 having a grid plate 24.
  • the cone-shaped member 23 is also provided with a wall member 25 and a dense phase of the catalyst and gypsum is maintained above the grid 24 as indicated generally by the numeral 26. Under the temperature conditions and in the presence of hydrocarbons and steam, the gypsum is converted substantially to calcium oxide and hydrogen sulfide.
  • a separation zone 23 is provided, which may be a cyclone separator or a plurality of cyclone separators in which the gas containing some of the calcium oxide and catalyst may be introduced by way of inlet 29.
  • the separation zone 2S separates the catalyst and calcium oxide from the gaseous products and causes the discharge thereof back into the dense bed 26 via dip leg 30.
  • the hydrogen sulfide-containing gases are then discharged from reaction zone 22 by way of line 31 into a hydrogen sulfide recovery zone 32 for separation and recovery of the hydrogen sulfide by way of line 33.
  • the recovered hydrogen sulfide may then be converted to free sulfur by any of the well-known processes such as by the Klaus process.
  • the separated gases which may contain carbon monoxide, carbon dioxide and some hydrogen, may be withdrawn from zone 32 by line 34 and introduced either into line 19 or into zone 22 as may be desired.
  • the hydrogen sulfide recovery zone may comprise a suitable absorption tower, such as one employing an ethanolamine, such as mono, di, or triethanolamine, for absorption of the hydrogen sulfide from the gas in line 31.
  • a suitable absorption tower such as one employing an ethanolamine, such as mono, di, or triethanolamine, for absorption of the hydrogen sulfide from the gas in line 31.
  • Other solutions may be used for recovery and separation of the hydrogen sulfide.
  • a solution of slightly acidic lead acetate may be employed, or the hydrogen sulfide-containing gases may be led into an absorber containing a solution of sodium hydroxide.
  • separation zone 37 which suitably may be of the gravity type but which may comprise a vibrating screen, a centrifugal separator, or an elutriation tower.
  • separation zone 37 is of the gravity type with the catalyst separating out by virtue of its difference in gravity from the calcium oxide.
  • the cobalt molybdate may have a specific gravity in the range from about 3 to about 4, depending on the carrier employed, while the calcium oxide has a specic gravity of about 2.2, which allows separation to be obtained readily.
  • The'catalyst separated fromthe'c'alciumoxide inzone' ⁇ 37 is Withdrawn therefrom by line 45- and introduced into a catalyst regeneration zone 46, airI being introduced into line 45 by way of line ⁇ 47', controlled by valve'S,t this air serving to transport the catalyst into zone i6-and also to provide oxygen for burning off any carbonaceous material deposited on the catalyst by-virtue of the reaction in zone 22.
  • a combustion operation is'sustained in zone 46 in which a temperature in the range from about 800 to about 1200 F. is employed to burn-ofi the carbonaceous material and to regenerate the catalyst.
  • the regenerated catalyst in a suspension of flue gas liows fromzone 4o by line 49- into a regenerated'catalyst zone Sii, line 4g terminating below the level 51 of the catalyst in zone t).
  • the flue gas is separated from zone 50 by way of separation zone 52 which returns any catalyst in the liuc gas back tothe catalyst level by way of dip leg 53, while the iiue gas may be removed from zone 50 by line Sd.
  • line 55 controlled by valve 56, introduces steam into the lower partv of zone S0 to sweep the catalyst free of any oxygen which may' remain in the regenerated catalyst before it is introduced into line 19 through line 20, controlled by ⁇ valve 57, and prior to introduction of the gypsum into'line 19 byrway of line 21controlled by valve 58.
  • the catalyst and the powdered gypsum suitably ⁇ have particle sizesin the range fromy about 100 to 3000 microns to allow ready fluidization thereof.
  • a major amount of the catalyst and the powdered gypsum has a particle size in the range from about 300 to about 1500.
  • the invention is quite advantageous and useful in that the calcium sulfate may be converted to lime' and hy# drogen sulfide employing hydrocarbon gases atasubstantially lower temperature thanwasipossible heretoforey by employing a sulfur-resistant catalyst of the. typeV mentioned supra. This quite important in that it is no longer necessary to employ the elevated temperatures which heretofore were necessary where hydrocarbon gases were used to convert calcium sulfate to gypsum.
  • the presence of an excess ofl these reactants serves to drive the reaction taking place'
  • the present invention may be carried out in apparatus other than that used by way of illustration.
  • a rotary type kiln or a granular bed reactor may be used or one of the so-called raining solids techniques may be empoyed.
  • a moving bed may be used in accordance with the present invention.
  • a steam to methane ratio of greater than 14 to 1 may be used, with a calcium sulfate to catalyst ratio ⁇ ranging from about 1 to 1 to about l0 to l may be employed-with the steam and methane or hydrocarbon gas always being in excess of that theoretically required to convert calcium sulfate to calcium oxide and hydrogen sulfide.
  • a method for producing lime and hydrogen sulfideA which comprises'contacting finely divided calcium sulfate with a natural gas hydrocarbon and steam in the presenceof cobalt mo'ybdate catalyst at a temperature withinl thel range from about 1200 to 1400 F. In the absence of free oxygen, the gas and steam beingV present in amounts in excess of theoretical, to form lime and hydrogen sulfide-containing gas, separating and'recovering said hydrogen sulfide from said gas in an absorption zone, separating said lime from the catalyst by gravity ⁇ and thencooling the separated lime in a cooling zone in the absence of free oxygen.
  • A- method for producing lime and hydrogen sulfide which comprises contacting finely divided calcium sulfate withnatural gas hydrocarbons and steam in the presence' of cobalt molybdate catalyst at a temperature withinthe' range from about l200 to 1400" F. and'at a pressure within the range from about atmospheric'to about 1000 ⁇ pounds per square inch gauge inA the absence of free cium sulfate and cobalt molybdate catalyst. suspending-- the mixture in natural gas and steam, contacting the suspension at a temperature within the range from about ⁇ 1200 to 1400 F.
  • the gas and steam being present in amounts in excess of theoretical, to form lime and hydrogen sulfide-containing gas, recovering hydrogen sulfide from said gas in an absorption zone, separating said lime from the catalyst by'grav ity, and then cooling the separated lime in a cooling zone in the absence of free oxygen.
  • method for producing lime andhydrogensulfide' which comprises forming a mixture of finely divided caicium sulfateY and cobalt-molybdate catalyst, contacting thev mixture with natural gas and steam at a" temperature" within the range from about 1200 to 1400' F. n the absence of free oxygen, the gas and steam being present in amounts in excess of theoretical, to form lime and hydrogen sulfide-containing gas, recovering hydrogen sulde from said gas in an absorption zone, and separating said lime from the catalyst by gravity.

Description

Feb. 7, 1961 P.s.v1LEs PRODUCTION oF LIME AND HYDROGEN suLFIDE Filed June`19, 195s INVENTOR.
PRENTlss s. VILEs,
A pu
United States Patent PRODUCTION OF LIME AND HYDROGEN SULFIDE Prentiss S. Viles, Baytown, Tex., assignor, by mesne assignments, to Esso Research and Engineering Company, Elizabeth, NJ., a corporation of Delaware Filed June 19, 1958, Ser. No. 743,050
7 Claims. (Cl. 23-181) The present invention is directed to a method for producing lime and hydrogen sulfide. More particularly, the invention is concerned with the production of lime and hydrogen sulfide from gypsum. In its more specific aspects, the invention is directed to a catalytic method for producing lime andhydrogen sulfide at a substantially reduced temperature.
' The present invention may be briefly described as a i method for producing lime and hydrogen sulfide which comprises forming a mixture of calcium sulfate and a sulfur-resistant catalyst and then contacting the mixture with a hydrocarbon gas and steam at a temperature within the range from about 850 to about 1500l F. in the absence of free oxygen, the gas and steam being present in amounts in excess of theoretical to form lime and hydrogen sulfide. The hydrogen sulfide and lime are separated from the catalyst and recovered and the recovered lime is then cooled in the absence of free oxygen.
The catalyst employed in the practice of the present invention is a sulfur-resistant catalyst which may be exemplified by cobalt molybdate. Other suitable sulfurresistant catalysts may be used, such as reducible salts of molybdenum and cobalt.
i Preferably, the sulfur-resistant catalyst is employed on a suitable support or carrier. For example, cobalt molybdate in an amount of 12 to 15 percent by weight deposited on a suitable carrier or support, such as alumina, is eminently suitable as a catalyst. The catalyst may comprise an amount within the range from about 1 to about 99 percent by weight of the active catalytic material with the remainder being the support.
Besides alumina, which may be a substantially purified alumina, such as gamma alumina, suitable supports may be zirconia, magnesia, and other materials, such as clay,;
and the like.
The temperatures employed in the practice of the present invention may range from about 850 to about 1500 F., with a preferred temperature in the range from about 1200 to l400 F. By virtue of employing a sulfur-re sistant catalyst, it is possible to produce lime and hydrogen sulfide at substantially reduced temperatures over that possible heretofore using a hydrocarbon gas.
Pressures suitably may range from about to about 1000 `pounds per square inch gauge. Advantageously, when a fiuidized operation is employed, pressures may range from about l0 up to about 200 pounds per square inch gauge.
The hydrocarbon gas employed in the practice of the present invention is suitably natural gas or the gaseous components thereof, such as methane, ethane, propane, and butane. It is preferred to use natural gas, although methane and the other gaseous components may be used.
The invention will be further illustrated by reference to the drawing in which the sole figure is a flow diagram of a preterred mode.
2,970,893 Patented Feb. 7, 1961 Referring now to the drawing, numeral 11 designates a charge line by way of which a gaseous hydrocarbon, such as methane, is introduced into the system by opening l valve 12. Discharging into line 11 is a charge line 13,
controlled by valve 14, by way of which steam is introduced in admixture with the methane. The steam and methane mixture then fiows into a furnace 15 provided with a heating coil 16 and gas burners 17, which raise the temperature of the mixture to a temperature in the range from about 850 to about 1500 F. The heated mixture fiows by way of line 18 into a large conduit 19 into which is introduced by way of line 20 a sufiicient amount of catalyst, such as cobalt molybdate on alumina, the catalyst being carried through line 19 by the velocity of flow of the mixture of methane and steam. The catalyst is admixed in line 19 with powdered gypsum introduced thereto by way of line 21, and the mixture of catalyst and powdered gypsum are then flowed by way of line 19 into a reaction zone 22, which is a large vessel provided with a cone-shaped member 23 having a grid plate 24. The cone-shaped member 23 is also provided with a wall member 25 and a dense phase of the catalyst and gypsum is maintained above the grid 24 as indicated generally by the numeral 26. Under the temperature conditions and in the presence of hydrocarbons and steam, the gypsum is converted substantially to calcium oxide and hydrogen sulfide.
Above the dense bed 26 is a disperse phase 27, which contains a small amount of the finely divided calcium oxide and perhaps some of the catalyst. To separate the catalyst and calcium oxide from the hydrogen sulfidecontaining gases, a separation zone 23 is provided, which may be a cyclone separator or a plurality of cyclone separators in which the gas containing some of the calcium oxide and catalyst may be introduced by way of inlet 29. The separation zone 2S separates the catalyst and calcium oxide from the gaseous products and causes the discharge thereof back into the dense bed 26 via dip leg 30. The hydrogen sulfide-containing gases are then discharged from reaction zone 22 by way of line 31 into a hydrogen sulfide recovery zone 32 for separation and recovery of the hydrogen sulfide by way of line 33. The recovered hydrogen sulfide may then be converted to free sulfur by any of the well-known processes such as by the Klaus process. The separated gases which may contain carbon monoxide, carbon dioxide and some hydrogen, may be withdrawn from zone 32 by line 34 and introduced either into line 19 or into zone 22 as may be desired.
The hydrogen sulfide recovery zone may comprise a suitable absorption tower, such as one employing an ethanolamine, such as mono, di, or triethanolamine, for absorption of the hydrogen sulfide from the gas in line 31. Other solutions may be used for recovery and separation of the hydrogen sulfide. For example, a solution of slightly acidic lead acetate may be employed, or the hydrogen sulfide-containing gases may be led into an absorber containing a solution of sodium hydroxide.
The catalyst and lime overfiow from dense bed 26 down through the annular space 35 and discharge from zone 22 by way of line 36 into a separation zone 37 which suitably may be of the gravity type but which may comprise a vibrating screen, a centrifugal separator, or an elutriation tower. In the drawing separation zone 37 is of the gravity type with the catalyst separating out by virtue of its difference in gravity from the calcium oxide. Thus, the cobalt molybdate may have a specific gravity in the range from about 3 to about 4, depending on the carrier employed, while the calcium oxide has a specic gravity of about 2.2, which allows separation to be obtained readily.
Steam is introduced into the upper portion of separation zone 37 by way of line38, controlled by valve 39, to decompose any residual' calcium sulfide which may be' present in the calcium oxide' and toexclude fr eeoxygen and/or air from contact with the lime; rliihe` calcium'oxide then liows fromr z oner37 by way ofl line 40 into a cooling zone 41 and finally the lime is recovered in the absence ofk air from zone 41v by line 42 Introduced into coolingzone 41 by way of line 43 isa cooling medium which may be steam-at* a lower temperature or other cooled gas, which is discharged by way of line 44; Suitably, the cooling medium introduced in line 4?? may be thev methane and steaml introduced into the system' byy lines 11 and 13 and passage of methane andf steam through zone 4l will serve to remove' he'a't from ther lime and to preheat'the'-methaneand steam'.
The'catalyst separated fromthe'c'alciumoxide inzone'` 37 is Withdrawn therefrom by line 45- and introduced into a catalyst regeneration zone 46, airI being introduced into line 45 by way of line` 47', controlled by valve'S,t this air serving to transport the catalyst into zone i6-and also to provide oxygen for burning off any carbonaceous material deposited on the catalyst by-virtue of the reaction in zone 22. A combustion operationis'sustained in zone 46 in which a temperature in the range from about 800 to about 1200 F. is employed to burn-ofi the carbonaceous material and to regenerate the catalyst.
The regenerated catalyst in a suspension of flue gas liows fromzone 4o by line 49- into a regenerated'catalyst zone Sii, line 4g terminating below the level 51 of the catalyst in zone t). The flue gas is separated from zone 50 by way of separation zone 52 which returns any catalyst in the liuc gas back tothe catalyst level by way of dip leg 53, while the iiue gas may be removed from zone 50 by line Sd.
In order to insure that the'catalyst is substantially free of oxygen, line 55, controlled by valve 56, introduces steam into the lower partv of zone S0 to sweep the catalyst free of any oxygen which may' remain in the regenerated catalyst before it is introduced into line 19 through line 20, controlled by` valve 57, and prior to introduction of the gypsum into'line 19 byrway of line 21controlled by valve 58.
The catalyst and the powdered gypsum suitably` have particle sizesin the range fromy about 100 to 3000 microns to allow ready fluidization thereof. A major amount of the catalyst and the powdered gypsum has a particle size in the range from about 300 to about 1500.
lt will be seen from the description taken with the drawing that an improved operation has been provided by way of which calcium sulfate,l suehas gypsum, is converted to lime and hydrogen sulfide. Lime and hydrogen sulfide may be used in many ways,` the hydrogen sulfide being used for conversion to elementary sulfur, while the lime may suitably be used in theV production of cement.
The invention is quite advantageous and useful in that the calcium sulfate may be converted to lime' and hy# drogen sulfide employing hydrocarbon gases atasubstantially lower temperature thanwasipossible heretoforey by employing a sulfur-resistant catalyst of the. typeV mentioned supra. This quite important in that it is no longer necessary to employ the elevated temperatures which heretofore were necessary where hydrocarbon gases were used to convert calcium sulfate to gypsum.
it is desirablev and necessary in the practice of the present invention that an excess of the hydrocarbon gas and steam be employed and that the amount of steam be in excess of that theoretically reactable` with the excess of hydrocarbony gas.
to' completion toform the desirable product;
The presence of an excess ofl these reactants serves to drive the reaction taking place' The present invention may be carried out in apparatus other than that used by way of illustration. For example, a rotary type kiln or a granular bed reactor may be used or one of the so-called raining solids techniques may be empoyed. Likewise, a moving bed may be used in accordance with the present invention.
lu the practice of the present invention employing steam, hydrocarbon gas and a sulfur-resistant catalyst to convert calcium sulfate tolime'and H28, it is possible to control the steamandhydrocarbon'gas ratio and'thecatalyst and calcium sulfate ratio to'eliminate back reactions of calcium oxide with carbon dioxide and sulfur dioxide which may be produced in the several reactions which may take p`ace. For example, a steam to methane ratio of greater than 14 to 1 may be used, with a calcium sulfate to catalyst ratio` ranging from about 1 to 1 to about l0 to l may be employed-with the steam and methane or hydrocarbon gas always being in excess of that theoretically required to convert calcium sulfate to calcium oxide and hydrogen sulfide. Y
it is also important in the practice of the presentinven'tion to conduct the reaction in the absence of free' oxygen and to maintain the lime free from contact with free oxygen. This prevents the undesirable formation of carbonates especially by excluding air from Contact with r the` lime.
`The nature and objects of the presentinvention having" been completely described and illustrated, whatiI wish to claim as new and useful and secure by Letters Patent is:
p l. A method for producing lime and hydrogen sulfideA which comprises'contacting finely divided calcium sulfate with a natural gas hydrocarbon and steam in the presenceof cobalt mo'ybdate catalyst at a temperature withinl thel range from about 1200 to 1400 F. In the absence of free oxygen, the gas and steam beingV present in amounts in excess of theoretical, to form lime and hydrogen sulfide-containing gas, separating and'recovering said hydrogen sulfide from said gas in an absorption zone, separating said lime from the catalyst by gravity` and thencooling the separated lime in a cooling zone in the absence of free oxygen.
2. Amethod in accordance with claim 1 in which the catalyst is supported cobalt molybdate.
3. A- method for producing lime and hydrogen sulfide which comprises contacting finely divided calcium sulfate withnatural gas hydrocarbons and steam in the presence' of cobalt molybdate catalyst at a temperature withinthe' range from about l200 to 1400" F. and'at a pressure within the range from about atmospheric'to about 1000` pounds per square inch gauge inA the absence of free cium sulfate and cobalt molybdate catalyst. suspending-- the mixture in natural gas and steam, contacting the suspension at a temperature within the range from about` 1200 to 1400 F. in the absence of free oxygen, the gas and steam being present in amounts in excess of theoretical, to form lime and hydrogen sulfide-containing gas, recovering hydrogen sulfide from said gas in an absorption zone, separating said lime from the catalyst by'grav ity, and then cooling the separated lime in a cooling zone in the absence of free oxygen.
5. A method in accordance with claim 4 in which the cataiyst is cobalt molybdate'supported on alumina.
6. method for producing lime andhydrogensulfide' which comprises forming a mixture of finely divided caicium sulfateY and cobalt-molybdate catalyst, contacting thev mixture with natural gas and steam at a" temperature" within the range from about 1200 to 1400' F. n the absence of free oxygen, the gas and steam being present in amounts in excess of theoretical, to form lime and hydrogen sulfide-containing gas, recovering hydrogen sulde from said gas in an absorption zone, and separating said lime from the catalyst by gravity.
7. A method in accordance with claim 6 in which the natural gas is methane.
6 References Cited in the le of this patent UNITED STATES PATENTS Zirngibl et al Sept. 5, 1939 Byrns Feb. 13, 1945 Nahin June 6, 1950 Burwell Apr. 3, 1956 Viles May 19, 1959

Claims (1)

1. A METHOD FOR PRODUCING LIME AND HYDROGEN SULFIDE WHICH COMPRISES CONTACTING FINELY DIVIDED CALCIUM SULFATE WITH A NATURAL GAS HYDROCARBON AND STEAM IN THE PRESENCE OF COBALT MOLYBDATE CATALYST AT A TEMPERATURE WITHIN THE RANGE FROM ABOUT 1200* TO 1400*F. IN THE ABSENCE OF FREE OXYGEN, THE GAS AND STEAM BEING PRESENT IN AMOUNTS IN EXCESS OF THEORETICAL, TO FORM LIME AND HYDROGEN SULFIDE-CONTAINING GAS, SEPARATING AND RECOVERING SAID HYDROGEN SULFIDE FROM SAID GAS IN AN ABSORPTION ZONE,
US743050A 1958-06-19 1958-06-19 Production of lime and hydropgen sulfids Expired - Lifetime US2970893A (en)

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3402998A (en) * 1964-01-15 1968-09-24 Arthur M. Squires Processes for desulfurizing fuels
US3460912A (en) * 1968-08-21 1969-08-12 Arthur M Squires Producing sulfur from calcium sulfate
US3481834A (en) * 1968-08-21 1969-12-02 Arthur M Squires Process and apparatus for desulfurizing fuels
US4431622A (en) * 1981-03-24 1984-02-14 Exxon Research And Engineering Co. Process for producing CO2, and CO2 so produced
FR2678601A1 (en) * 1991-07-01 1993-01-08 Commissariat Energie Atomique PROCESS FOR THE PREPARATION OF SULFIDE AND SULFURED AMINO ACIDS 35.
US20090247392A1 (en) * 2008-03-26 2009-10-01 Ghorishi S Behrooz In-situ regeneration of a catalyst masked by calcium sulfate

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2171966A (en) * 1935-07-03 1939-09-05 Ig Farbenindustrie Ag Process for reducing kieserite
US2369432A (en) * 1939-01-24 1945-02-13 Union Oil Co Desulphurization catalysts
US2510189A (en) * 1948-02-16 1950-06-06 Union Oil Co Supported catalyst and preparation thereof
US2740691A (en) * 1953-05-25 1956-04-03 Univ Oklahoma Res Inst Process for the recovery of lime and hydrogen sulfide from calcium sulfate
US2887363A (en) * 1956-09-28 1959-05-19 Exxon Research Engineering Co Conversion of methane to produce hydrogen sulfide

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2171966A (en) * 1935-07-03 1939-09-05 Ig Farbenindustrie Ag Process for reducing kieserite
US2369432A (en) * 1939-01-24 1945-02-13 Union Oil Co Desulphurization catalysts
US2510189A (en) * 1948-02-16 1950-06-06 Union Oil Co Supported catalyst and preparation thereof
US2740691A (en) * 1953-05-25 1956-04-03 Univ Oklahoma Res Inst Process for the recovery of lime and hydrogen sulfide from calcium sulfate
US2887363A (en) * 1956-09-28 1959-05-19 Exxon Research Engineering Co Conversion of methane to produce hydrogen sulfide

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3402998A (en) * 1964-01-15 1968-09-24 Arthur M. Squires Processes for desulfurizing fuels
US3460912A (en) * 1968-08-21 1969-08-12 Arthur M Squires Producing sulfur from calcium sulfate
US3481834A (en) * 1968-08-21 1969-12-02 Arthur M Squires Process and apparatus for desulfurizing fuels
US4431622A (en) * 1981-03-24 1984-02-14 Exxon Research And Engineering Co. Process for producing CO2, and CO2 so produced
FR2678601A1 (en) * 1991-07-01 1993-01-08 Commissariat Energie Atomique PROCESS FOR THE PREPARATION OF SULFIDE AND SULFURED AMINO ACIDS 35.
EP0522918A1 (en) * 1991-07-01 1993-01-13 Commissariat A L'energie Atomique Process for the preparation of sulfides and amino acids labelled with sulfur-35
US5344767A (en) * 1991-07-01 1994-09-06 Commissariat A L'energie Atomique Process for preparing sulfides and amino acids labeled with sulfur-35
US20090247392A1 (en) * 2008-03-26 2009-10-01 Ghorishi S Behrooz In-situ regeneration of a catalyst masked by calcium sulfate
US8048818B2 (en) * 2008-03-26 2011-11-01 Babcock & Wilcox Power Generation Group, Inc. In-situ regeneration of a catalyst masked by calcium sulfate
TWI471171B (en) * 2008-03-26 2015-02-01 Babcock & Wilcox Power Generat In-situ regeneration of a catalyst masked by calcium sulfate
CN101543793B (en) * 2008-03-26 2015-05-06 巴布科克和威尔科克斯能量产生集团公司 In-situ regeneration of a catalyst masked by calcium sulfate

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